EP0468540B1 - Verringerung der Schadstoffemission in Rauchgasen von Kohlefeuerungen - Google Patents

Verringerung der Schadstoffemission in Rauchgasen von Kohlefeuerungen Download PDF

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Publication number
EP0468540B1
EP0468540B1 EP91115149A EP91115149A EP0468540B1 EP 0468540 B1 EP0468540 B1 EP 0468540B1 EP 91115149 A EP91115149 A EP 91115149A EP 91115149 A EP91115149 A EP 91115149A EP 0468540 B1 EP0468540 B1 EP 0468540B1
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EP
European Patent Office
Prior art keywords
reagent
baghouse
flue gas
gas stream
ammonia
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP91115149A
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English (en)
French (fr)
Other versions
EP0468540A1 (de
Inventor
John B. Doyle
Ed A. Pirsh
William Downs
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Babcock and Wilcox Co
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Babcock and Wilcox Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Babcock and Wilcox Co filed Critical Babcock and Wilcox Co
Publication of EP0468540A1 publication Critical patent/EP0468540A1/de
Application granted granted Critical
Publication of EP0468540B1 publication Critical patent/EP0468540B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/101—Baghouse type
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Definitions

  • This invention relates to controlling emission of pollutants from coal-fired boiler systems, for example in coal-fired electric power plants.
  • fly-ash is separated from flue gas by filtration, i.e. the fly-ash is collected on the upstream side of tubularly shaped fabric filter bags as the gas is directed through the filter bags.
  • the flue gas passes through a filter bag, typically from the inside out, and the fly-ash is collected as so-called filter cake.
  • the material collected on the bag becomes part of the filtering medium. After a certain build-up of filter cake over the course of operation, the bags must be cleaned to avoid excessive pressure drop in order to maintain proper gas volume flow.
  • the use of a bag filterhouse gives the power generator company the option of switching coals since bag filterhouse collection efficiency is relatively insensitive to fuel characteristics.
  • US Patent No.US-A-4309386 discloses a system in which a hot catalytic baghouse (greater than 316°F (600°F)) is used for simultaneous particulate removal and NO x reduction.
  • a hot catalytic baghouse greater than 316°F (600°F)
  • filter bags of the baghouse are treated with a catalyst to facilitate a selective catalytic reduction process while simultaneously filtering out particulate matter from the gas stream.
  • the baghouse is situated downstream from an ammonia injection system. In the baghouse, the flue gas stream is exposed to the treated bags to effect NO x removal.
  • that system has several potential shortcomings.
  • bags impregnated with the catalyst tend to have an unduly limited life span, necessitating periodic replacement of the entire bag, and the catalyst is subject to SO x poisoning which can lead to loss of ability to reduce NO x in the presence of gases containing high quantities of SO x .
  • a method of controlling emission of pollutants from a coal-fired boiler system which system includes a boiler, an economiser, a fabric filter baghouse and an air heater in a serial fluid communication path, by removing, in a temperature range of 316°C to 427°C (600°F to 800°F), SO x , NO x and particulates from a combustion flue gas stream passing through said path, the method comprising the steps of:
  • a suitable reagent can be pneumatically injected into a boiler in fine powder form, in a temperature zone below the melting point of the reagent, upstream of a hot baghouse which is operating in a temperature range of approximately 316°C to 427°C (600°F to 800°F) and which is located between an exit of an economiser of the boiler and an air heater.
  • Ammonia is also injected in this vicinity.
  • a reaction between the NO x and ammonia converts the NO x to harmless nitrogen gas and a reaction between SO x and the reagent produces a solid particulate which continues to flow with the flue gas.
  • the mixture of reactants, reaction products and flue gases continues to flow to the baghouse, where the particulates are separated from the flue gas.
  • the injection technique advantageously provides an extended time for reaction of the reagent and the SO x and NO x as the flue gas stream flows from the injection position to fabric filter bags of the baghouse. Further reaction takes place as the solids are collected in the filter bags as filter cake and the flue gases continue to pass through the filter cake.
  • the reagent is removed from the baghouse, along with the fly-ash,for regeneration. Poisoning of the catalyst with SO x is no longer a problem since the method seeks to achieve reaction of the reagent with SO x to remove the sulphur oxides from the gas stream and the reaction is otherwise acceptable due to the continuous replenishment of the reagent by regeneration.
  • the drawing shows a coal-fired boiler 10 that includes an economiser 12 which is designed, as is well known, to remove heat from the combustion flue gases after the gases leave steam-generating and superheating sections of the boiler 10.
  • An outlet of the economiser 12 is connected through a flue gas conduit 14 to a baghouse 16 in which particulates are collected in filter bags (not shown).
  • the treated gas is discharged from the baghouse 16 through a conduit 18 to an air preheater 20 and then through a conduit 22 to a stack 24 for ultimate discharge to the atmosphere.
  • Injection lines 26,28 are provided for injecting a solid reagent which is also a catalyst and ammonia (NH3), respectively, into a zone, having a temperature below the reagent melting point,upstream of the baghouse 16.
  • a solid reagent which is also a catalyst and ammonia (NH3), respectively
  • the solid reagent and ammonia are injected upstream of the economiser 12, i.e. intermediate the boiler 10 and the economiser 12.
  • the ammonia is preferably injected between a primary superheater and the economiser 12 as placement further upstream would result in excessive loss of ammonia by oxidation.
  • the temperature at the economiser inlet will typically be between 371°C and 538°C (700°F and 1000°F), and the preferred operating range is 316°C to 427°C (600°F to 800°F). Reagents are selected which will not react with ammonia in this temperature range.
  • the combustion flue gas which contains particulates, SO x and NO x , reacts with the reagent as it flows through the economiser 12 and to the baghouse 16. As the gas flows from the injection point through the baghouse 16, the reagent reacts with SO x and NO x and ammonia. The reagent reacts further as it collects in the filter bags and the flue gas passes through it.
  • the reagent is alkali and alkaline earth hydroxides, carbonates or oxides.
  • the spent reagent material is removed from the baghouse 16 with the fly-ash.
  • the spent material contains sulphur from the flue gas in the form of sulphates and sulphites.
  • the spent material and fly-ash are then fed into a fluid bed gasifier 30 where coal is added as a fuel source and the temperature of the sulphated spent material is raised to a level where the sulphur is driven off in the form of sulphur dioxide and hydrogen sulphide.
  • the reagent is then removed from the gas stream with the fly-ash via a particulate collector 32, such as a secondary baghouse,precipitator, or high efficiency cyclone.
  • the collected solids are then added to water in a mixing tank 34 to form a slurry.
  • the reagent goes into solution.
  • the slurry is then directed to a solid separator 36, such as a belt filter or centrifuge, where the ash is removed from the system.
  • a solid separator 36 such as a belt filter or centrifuge, where the ash is removed from the system.
  • the solution containing the regenerated reagent is then recycled as make-up back to the boiler 10.
  • a drier 40 may be required prior to injecting the reagent into the boiler.
  • the spent gas from the fluid bed gasifier 30 may be taken to a Klaus plant 38 where the SO2 and H2S may be recovered in the form of elemental sulphur. A portion of the steam produced in the fluid bed gasifier 30 may be used for the operation of the Klaus plant 38.
  • the low J(Btu) gas would then be sent back to the boiler 10 as additional fuel with pulverised coal from a pulveriser 42 or could be used for other plant process requirements. There is a possibility that this gas could be used in the production of ammonia which in turn could be used as the make-up for the NO x reduction process.

Claims (3)

  1. Verfahren zur Steuerung der Schadstoffemission aus einem kohlebefeuerten Kesselsystem, welches einen Kessel (10), einen Rauchgasvorwärmer (12), ein Tuchfiltersackgehäuse (16) und einen Lufterhitzer (20) in einer Reihe auf eine Fließmittelverbindungsweg einschließt, durch Entfernung von SOx, NOx und Feinstoffen in einem Temperaturbereich von 316 bis 427 °C (600 bis 800 °F) aus einem Verbrennungsrauchgasstrom, der diesen Weg passiert, wobei das Verfahren die Stufen umfaßt, in denen man
    a) ein Reagenz, welches auch ein Katalysator ist, der aus der Gruppe ausgewählt ist, die aus Alkali- und Erdalkalicarbonaten oder -oxiden in Pulverform besteht, und Ammoniak dem Verbrennungsrauchgasstrom aufstromwärts von dem Tuchfiltersackgehäuse (16) zwischen dem Kessel und dem Sackgehäuse in einer Temperaturzone mit einer Temperatur unterhalb des Schmelzpunktes des Reagenz zusetzt (26, 28),
    b) etwas von dem Reagenz und Ammoniak mit dem SOx und NOx unter Bildung von Reaktionsprodukten umsetzt, während der Rauchgasstrom zu dem Sackgehäuse (16) geht,
    c) die Feinstoffe, die Reaktionsprodukte und das Reagenz aus dem Rauchgas in dem Temperaturbereich durch Filtration in dem Sackgehäuse (16) unter Bildung eines Filterkuchens abtrennt,
    d) den Rauchgasstrom durch den Filterkuchen führt, um weiteres Reagenz und Ammoniak mit dem SOx und NOx unter Bildung weiterer Reaktionsprodukte und von gereinigtem Gas umzusetzen und
    e) das gereinigte Gas aus dem Sackgehäuse (16) durch den Lufterhitzer (20) abbläst.
  2. Verfahren nach Anspruch 1, bei dem die Reaktionsstufe (b) eine Umsetzung von etwas des Reagens und Ammoniak mit dem SOx und NOx umfaßt, um Reaktionsprodukte zu bilden, während der Rauchgasstrom durch den Rauchgasvorwärmer (12) zu dem Sackgehäuse (16) geht.
  3. Verfahren nach Anspruch 1 oder Anspruch 2, bei dem man Reagens aus dem Filterkuchen wiedergewinnt, indem man den Filterkuchen auf eine ausreichende Temperatur erhitzt (30), um Schwefeldioxid und Schwefelwasserstoff aus dem Filterkuchen zu verflüchtigen und auszutreiben und zurückbleibende, aus dem Filterkuchen gewinnbares Sulfid enthaltende Feststoffe zu bilden und zurückbleibende, gewinnbares Reagens enthaltende Feststoffe zu bilden, die gesammelten Feststoffe mit Wasser aufschlämmt, das gewinnbare Reagens von den Feststoffen abtrennt (32), wobei die Zugabestufe (a) ein Überführen des gewonnenen Reagens in den Verbrennungsgasstrom einschließt.
EP91115149A 1986-11-19 1987-09-07 Verringerung der Schadstoffemission in Rauchgasen von Kohlefeuerungen Expired - Lifetime EP0468540B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US06/932,754 US4793981A (en) 1986-11-19 1986-11-19 Integrated injection and bag filter house system for SOx -NOx -particulate control with reagent/catalyst regeneration
EP87307884A EP0268353B1 (de) 1986-11-19 1987-09-07 Verringerung der Schadstoffemission in Rauchgasen von Kohlefeuerungen
US932754 1992-08-20

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
EP87307884.4 Division 1987-09-07

Publications (2)

Publication Number Publication Date
EP0468540A1 EP0468540A1 (de) 1992-01-29
EP0468540B1 true EP0468540B1 (de) 1994-11-09

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Application Number Title Priority Date Filing Date
EP87307884A Expired - Lifetime EP0268353B1 (de) 1986-11-19 1987-09-07 Verringerung der Schadstoffemission in Rauchgasen von Kohlefeuerungen
EP91115149A Expired - Lifetime EP0468540B1 (de) 1986-11-19 1987-09-07 Verringerung der Schadstoffemission in Rauchgasen von Kohlefeuerungen

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EP87307884A Expired - Lifetime EP0268353B1 (de) 1986-11-19 1987-09-07 Verringerung der Schadstoffemission in Rauchgasen von Kohlefeuerungen

Country Status (9)

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US (1) US4793981A (de)
EP (2) EP0268353B1 (de)
JP (1) JPS63130125A (de)
CN (1) CN1010280B (de)
CA (1) CA1273474A (de)
DE (3) DE3780411T4 (de)
DK (1) DK605787A (de)
ES (2) ES2033317T3 (de)
NO (1) NO168233C (de)

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NO168233B (no) 1991-10-21
EP0268353B1 (de) 1992-07-15
CN87107195A (zh) 1988-07-27
JPS63130125A (ja) 1988-06-02
CA1273474A (en) 1990-09-04
DE3780411T4 (de) 1995-08-10
CN1010280B (zh) 1990-11-07
NO873641D0 (no) 1987-08-28
ES2033317T3 (es) 1993-03-16
DE3750750T2 (de) 1995-03-16
EP0268353A1 (de) 1988-05-25
DE3780411D1 (de) 1992-08-20
DE3750750D1 (de) 1994-12-15
NO873641L (no) 1988-05-20
EP0468540A1 (de) 1992-01-29
NO168233C (no) 1992-01-29
DK605787A (da) 1988-05-20
DE3780411T2 (de) 1992-12-24
DK605787D0 (da) 1987-11-18
ES2063424T3 (es) 1995-01-01
JPH045486B2 (de) 1992-01-31
US4793981A (en) 1988-12-27

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